WO2005065823A1 - Catalyseur d'hydrogenation et de desulfuration pour hydrocarbure de petrole et procede d'hydrogenation et de desulfuration utilisant ce catalyseur - Google Patents

Catalyseur d'hydrogenation et de desulfuration pour hydrocarbure de petrole et procede d'hydrogenation et de desulfuration utilisant ce catalyseur Download PDF

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WO2005065823A1
WO2005065823A1 PCT/JP2005/000435 JP2005000435W WO2005065823A1 WO 2005065823 A1 WO2005065823 A1 WO 2005065823A1 JP 2005000435 W JP2005000435 W JP 2005000435W WO 2005065823 A1 WO2005065823 A1 WO 2005065823A1
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Prior art keywords
catalyst
hydrodesulfurization
group
mass
metal
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PCT/JP2005/000435
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English (en)
Japanese (ja)
Inventor
Hideshi Iki
Kazuaki Hayasaka
Shinya Takahashi
Kazuo Fukazawa
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Nippon Oil Corporation
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Priority claimed from JP2004004768A external-priority patent/JP4249632B2/ja
Priority claimed from JP2004216337A external-priority patent/JP2006035052A/ja
Application filed by Nippon Oil Corporation filed Critical Nippon Oil Corporation
Priority to EP05703674A priority Critical patent/EP1702682A4/fr
Publication of WO2005065823A1 publication Critical patent/WO2005065823A1/fr
Priority to US11/456,160 priority patent/US20060249429A1/en
Priority to KR1020067015820A priority patent/KR101218947B1/ko

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063—Titanium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/882—Molybdenum and cobalt
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/883—Molybdenum and nickel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14—Phosphorus; Compounds thereof
    • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
    • B01J27/19—Molybdenum
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/12—Silica and alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64—Pore diameter
    • B01J35/647—2-50 nm
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/66—Pore distribution

Definitions

  • the present invention relates to a petroleum hydrocarbon hydrodesulfurization catalyst and a hydrodesulfurization method. Specifically, the present invention relates to a method for desulfurizing petroleum hydrocarbons under specific reaction conditions and under specific reaction conditions when desulfurizing petroleum hydrocarbons containing sulfur components by hydrotreating.
  • benzothiophenes for kerosene fractions and alkyl-substituted dibenzothiophenes having multiple methyl groups as substituents represented by 4,6-dimethyldibenzothiophene for gas oil fractions are particularly poorly reactive.
  • this is an obstacle to proceeding with desulfurization to a lower sulfur region such as a sulfur content of 10 mass ppm.
  • a method of increasing the number of active sites by increasing the amount of active metal supported can be considered.However, even if a porous support having a high surface area mainly composed of alumina is used, the active metal can be supported. There is a limit to the amount, and if it is excessively supported, the active metal will aggregate and the activity will be reduced. In addition, excessive loading of the active metal blocked the pores of the catalyst and prevented the catalyst from exhibiting sufficient activity, or had a technical limitation that the activity decreased significantly.
  • Nitrogen is present as an organic nitrogen compound, and is said to contain, for example, amine, pyridine, pyrrole, indole, quinoline, phenol, and derivatives thereof. It is known that such nitrogen compounds adsorb to the catalyst and inhibit their activity (for example, see Non-Patent Document 3), and depending on the type of crude oil and the refining process, treat hydrocarbons containing a large amount of nitrogen compounds. As long as the conventional technology is used, the presence of nitrogen compounds is regarded as one of the major obstacles to the progress of desulfurization. -
  • the present invention provides an inorganic porous carrier containing alumina as a main component, wherein at least one kind of metal selected from Group 8 metals of the periodic table and an active metal selected from Group 6A metals of the Periodic Table are used as active metals. At least one metal is contained in the molar ratio of [VIII metal oxide] / [Group 6A metal oxide] in the range of 0.15 to 0.265, and A hydrodesulfurization catalyst for petroleum hydrocarbons, characterized in that the content of Group 6A metal is in the range of 20 to 30% by mass relative to the weight of the catalyst in terms of oxide.
  • the present invention also relates to the petroleum hydrocarbon hydrodesulfurization catalyst as described above, wherein the inorganic porous carrier further contains 0.5 to 10% by mass of phosphorus as oxide relative to the carrier. .
  • the present invention relates to a method for hydrodesulfurizing petroleum hydrocarbons, which comprises hydrodesulfurizing petroleum hydrocarbons using the hydrodesulfurization catalyst.
  • a method for hydrodesulfurizing petroleum hydrocarbons which comprises hydrodesulfurizing petroleum hydrocarbons using the hydrodesulfurization catalyst.
  • the catalyst in the present invention uses an inorganic porous substance containing alumina as a main component as a carrier.
  • the content of alumina is preferably at least 80% by mass, more preferably at least 85% by mass, further preferably at least 90% by mass with respect to the carrier. It is.
  • Alumina is a porous carrier particularly suitable for providing a pore volume suitable for diffusing hydrocarbon molecules having a boiling point of 240 to 380 ° C, and having an alumina content of more than 80% by mass. If the amount is small, it will be difficult to obtain a sufficient carrier pore volume.
  • the inorganic porous carrier those further containing phosphorus are preferable.
  • the catalyst By adding phosphorus, the catalyst can be made less susceptible to the inhibition of the desulfurization reaction by the nitrogen compound.
  • the content of phosphorus contained in the inorganic porous support is preferably from 0.5 to 1 0 weight 0/0 against the carrier in terms of oxide, more preferably from 1 to 9 mass%, 2 ⁇ more preferably 6 mass 0/0. If the phosphorus content is less than 0.5% by mass in terms of oxide, sufficient desulfurization activity cannot be exhibited, and the effect of improving nitrogen resistance is small.
  • the properties increase, and hydrocarbons are decomposed, which may reduce the yield and decrease the activity due to coke generation accompanying the decomposition.
  • the carrier is a component other than alumina and phosphorus, and at least one selected from the group consisting of Si, Ti, Zr, Mg, Ca, and B. Is preferably contained in the range. The content is more preferably from 1.2 to 9% by mass, and still more preferably from 1.5 to 8% by mass. These elements are preferably Si, Ti, Zr, and B, more preferably Si, Ti, and B, and particularly preferably Si. Further, these elements can be used in combination.
  • the content of these elements is less than 1% by mass in terms of oxides, the desulfurization activity and nitrogen resistance will be reduced. If the content exceeds 10% by mass, the acidity of the carrier will become strong, resulting in decomposition, etc. There is a concern that undesirable side reactions may occur.
  • the method for preparing alumina as the main component of the carrier is not particularly limited. For example, it can be obtained by a method of neutralizing or hydrolyzing an aluminum salt and an aluminate, or via an alumina intermediate obtained by a method of hydrolyzing an aluminum amalgam or aluminum alcoholate. . Also, commercially available alumina intermediate Body, boehmite powder may be used.
  • the method for incorporating phosphorus into the carrier there is no particular limitation on the method for incorporating phosphorus into the carrier.
  • a method of adding phosphoric acid or an alkali salt of phosphoric acid at the time of preparing alumina is preferably employed.
  • the aluminum hydroxide gel containing phosphorus may be added to an aqueous aluminum solution beforehand, or may be added to the prepared aluminum hydroxide gel, or water or alumina may be added to a commercially available alumina intermediate or boehmite powder. It may be added to the step of kneading by adding an acidic aqueous solution.
  • the step of preparing the aluminum hydroxide gel already contains phosphorus. Note that phosphorus is present in the carrier in the form of an oxide.
  • the carrier contains an element selected from Si, Ti, Zr, Mg, Ca, and B.
  • it may be impregnated and supported in a solution state.
  • it is added at any stage before firing alumina.
  • These elements are present in the carrier in the form of oxides.
  • the active metal to be supported on the carrier at least one metal selected from Group 8 metals of the periodic table and at least one metal selected from Group 6A metals of the periodic table are used.
  • Combinations of Group 8 metals and Group 6A metals include Co—Mo, Ni_Mo, Co—W, Ni—W, Co—Ni—Mo, and Co_N'i—W Is preferable, and a combination of Co—Mo or Ni—Mo is more preferable.
  • the content of the Group 6A metal is preferably in the range of 20 to 30% by mass, more preferably 21 to 26% by mass, more preferably 22 to 30% by mass of the catalyst in terms of oxide. 2525% by mass. If the amount is less than 20% by mass, the active sites are small and sufficient desulfurization activity cannot be exhibited. If the amount is more than 30% by mass, metal aggregation occurs, and the desulfurization activity may be reduced.
  • the loading ratio of Group 8 metal to Group 6A metal is 0.105 to 0.265 in molar ratio of [Group 8 metal oxide] / [Group 6A metal oxide]. It is necessary to be. It is preferably 0.11 to 0.20, more preferably 0.15 to 0.250, and still more preferably 0.120 to 0.220. If the molar ratio is less than 0.15, the co-catalyst effect of the Group 8 metal cannot be sufficiently exhibited, and the desulfurization activity will be reduced. On the other hand, if the molar ratio is greater than 0.265, sufficient hydrogenation activity cannot be exerted, and the effect of the nitrogen compound on the activity becomes large, and the desulfurization activity and nitrogen resistance may decrease. There is.
  • the total content of the Group 8 metal and the Group 6 metal is preferably 22% by mass or more, more preferably 23% by mass or more, even more preferably 25% by mass or more in terms of oxide based on the weight of the catalyst. If the content is less than 22% by mass, there is a concern that sufficient desulfurization activity cannot be exerted because the amount of active metal is small.
  • phosphorus is supported together with the active metal as an active ingredient.
  • the amount of phosphorus supported on the carrier is preferably in the range of 0.105 to 0.255, more preferably 0.15, in terms of the molar ratio of [Philic acid pentate] Z [Group 6A metal oxide]. It is from 120 to 0.240, most preferably from 0.130 to 0.205. If the molar ratio is less than 0.105, the effect of phosphorus cannot be sufficiently exerted.If the molar ratio is greater than 0.255, the acidity of the catalyst becomes strong and the decomposition reaction and coke formation reaction are accelerated. There is a possibility.
  • the method for supporting the group 8 metal and the group 6A metal, which are active metal components, on the carrier is not particularly limited, and a known method applied in producing a usual hydrodesulfurization catalyst can be used.
  • a method of impregnating a carrier with a solution containing a salt of an active metal is preferably employed.
  • an equilibrium adsorption method, a Pore-filinng method, an Incipinet-wetness method, and the like are also preferably employed.
  • the pore-filling method is a method in which the pore volume of a carrier is measured in advance and the same volume of a metal salt solution is impregnated.
  • the impregnation method is not particularly limited. It can be impregnated by an appropriate method depending on the amount of the metal supported and the physical properties of the carrier.
  • the method of supporting phosphorus on the carrier may be carried out by coexisting with an aqueous solution containing the aforementioned Group 8 metal or Group 6A metal. After loading, it may be loaded sequentially.
  • the above-mentioned method such as the equilibrium adsorption method is preferably employed.
  • the hydrodesulfurization catalyst of the present invention has an average pore size of the catalyst determined by the BET method using nitrogen.
  • the radius is in the range of 30 to 45 A, more preferably in the range of 32 to 4 OA. If the molecular weight is smaller than 3 OA, the diffusion of the reactive molecule in the pores is not sufficient, and the activity becomes low. On the other hand, if it is larger than 45 A, the surface area of the catalyst becomes too small to exert a sufficient desulfurization activity, which is not preferable.
  • the pore volume of the catalyst having a pore radius of 3 OA or less is preferably in the range of 13 to 33%, more preferably in the range of 15 to 30% of the total pore volume.
  • the pore volume occupied by the catalyst having a pore radius of 45 A or more is preferably in the range of 5 to 20%, more preferably in the range of 8 to 15%, and still more preferably in the range of 12 to 1%. It is in the range of 5%.
  • the pores in this region are considered to be important pores that determine the degree to which the reaction molecules reach the reaction active site.If it is less than 5%, the diffusion of the reaction molecules may not be sufficient and the activity may be reduced. There is. However, if it is more than 20%, there is a concern that the surface area of the catalyst itself decreases and the activity decreases.
  • hydrodesulfurization of petroleum hydrocarbons is performed using the above-mentioned catalyst.
  • Examples of the petroleum hydrocarbon to which the catalyst of the present invention is applied include a crude distillation apparatus, a crude distillation apparatus, and a pyrolysis apparatus for a crude oil containing at least 80% by volume of a fraction having a boiling point of 140 to 550 ° C. , Catalytic cracking, and fractions produced in petroleum refining processes such as hydrotreating.
  • the hydrodesulfurization catalyst of the present invention is suitable for desulfurization from sulfur molecules having a structure such as thiophenes, benzothiophenes, and dibenzothiophenes, and particularly has a boiling point of 240 to 380 ° C., which is a gas oil fraction.
  • Petroleum hydrocarbons can include fractions obtained by distillation of crude oil, as well as fractions obtained by thermal cracking and catalytic cracking reactions, but more than 50% by volume of gas oil fractions are straight-run. Light oil is preferred And more preferably 70% by volume or more.
  • Pyrolysis gas oils and catalytic cracking gas oils contain higher amounts of olefins and aromatics than straight-run gas oils.When the proportion of these fractions increases, the reactivity tends to decrease and the hue of the resulting oil tends to deteriorate. is there. Similarly from the reason, 5 0 volume in kerosene fraction. / 0 or more is preferably straight kerosene, and more preferably 70% by volume or more.
  • the properties of such a gas oil fraction generally include a total aromatic content of 20 to 30% by volume and a sulfur content of 0.8 to 2% by mass. /.
  • the nitrogen content is 100-500 mass ppm.
  • the total aromatic content is 1 to 5 to 25% by volume, and the sulfur content is 0.1 to 1 mass. /.
  • the nitrogen content is generally about 1 to 20 mass ppm.
  • the values of the distillation properties shown here are values measured in accordance with the method described in JIS K 2254 '' Evaporation test method for petroleum products'.
  • the sulfur content can be reduced to 10 mass ppm or less, preferably 7 mass ppm or less by hydrodesulfurizing such a petroleum hydrocarbon using the catalyst of the present invention. .
  • the kerosene fraction is used in a predetermined amount mixed with the diesel fraction in order to adjust the properties of diesel fuel such as fluidity in cold regions. For this reason, by hydrodesulfurizing such a kerosene fraction to a sulfur content of 10 mass ppm or less, the above-described sulfur reduction effect can be exhibited in diesel engine exhaust gas treatment. Furthermore, when used as fuel for heating appliances such as stoves, the use of kerosene with a sulfur concentration of 10 'mass ppm or less can be expected to significantly reduce the generation of harmful sulfur oxides and the like.
  • the nitrogen concentration can be reduced to 3 mass ppm or less, preferably 1 mass ppm or less.
  • nitrogen is known to be a catalyst poison.
  • the operating conditions of the hydrodesulfurization reaction can be made mild and contribute to the reduction of operating costs.
  • the extremely effective desulfurization reaction is progressing because the generated oil nitrogen concentration can be reduced to 3 mass ppm or less.
  • the reaction inhibition by the nitrogen component is large in the reaction tower where the hydrodesulfurization reaction is progressing. Efficient reaction progress is hindered, necessitating higher temperatures or higher hydrogen partial pressures and longer catalyst-oil contact times.
  • the catalyst of the present invention contains at least 80% by volume of a petroleum hydrocarbon fraction having a boiling point of 240 to 380 ° C, which is a gas oil fraction.
  • a petroleum hydrocarbon fraction having a boiling point of 240 to 380 ° C, which is a gas oil fraction.
  • the nitrogen content is 100 ppm by mass or more
  • the effect of nitrogen resistance can be more exerted, preferably 120 ppm by mass or more, and more preferably 150 ppm by mass.
  • the effect becomes remarkable at mass ppm or more, more preferably at 200 mass ppm or more.
  • nitrogen resistance For petroleum hydrocarbons containing a kerosene fraction with a boiling point range of 140 to 240 ° C of 80% by volume or more, when nitrogen content is 4% by mass or more, nitrogen resistance The effect is more pronounced, preferably at least 6 ppm by mass, more preferably at least 8 ppm by mass, even more preferably at least 10 ppm by mass.
  • the sulfur concentration refers to a petroleum-based concentration measured in accordance with the method described in JISK2541 “Sulfur content test method” or ASTM-D5453. It means the mass content of sulfur based on the total amount of hydrocarbons.
  • Nitrogen content refers to petroleum hydrocarbons measured in accordance with the method described in JISK 2609 “Nitrogen content test method” or ASTM-D 4629, D-5762. It means the mass content of nitrogen based on the total amount.
  • the petroleum hydrocarbon used as the feedstock has a volume of 80 volumes of a fraction with a boiling point of 240-380 ° C. / 0 or more, by performing the hydrodesulfurization treatment using the catalyst of the present invention, the total aromatic content in the product oil is also 18% by volume or less, preferably 16% by volume or less. Can be reduced.
  • Aromatic content is said to be one of the causes of particulates contained in diesel engine exhaust gas. When the total aromatic content exceeds 18% by volume, particulate generation tends to increase. is there.
  • Method means the sum of the volume percentages (volume%) of the respective aromatic components measured according to the method described in“ Method ”.
  • the petroleum hydrocarbon as the feedstock oil contains a fraction having a boiling point of 240 to 380 ° C. of 80% by volume or more
  • hydrodesulfurization treatment using the catalyst of the present invention is performed.
  • the hue of the produced oil can be reduced to 1.0 or less in ASTM color. If it exceeds 1.0, the hue as light oil will be yellow or close to brown, and the commercial value will decrease.
  • the coloring in the hydrodesulfurization treatment is related to the desulfurization reaction temperature, but according to the present invention, such a high reaction temperature and severe operating conditions are not adopted. As a result, stable and colorless gas oil with high commercial value can be produced.
  • the ASTM color means a hue measured according to the method described in JISK250 “Color Test Method”.
  • general reaction conditions can be adopted.
  • LHSV is preferably 0. 3 ⁇ 5.
  • O h- 1 and more preferable properly is 0. 3 5 ⁇ 4.
  • L 113 is less than 0.3 h- 1 , the reactor volume for obtaining a certain amount of oil flow becomes extremely large, so huge equipment investment such as installation of a reactor may be required. .
  • the LHSV is greater than 5.0 h- 1 , the contact time between the catalyst and oil will be short, and the desulfurization reaction will not proceed sufficiently, and the effects of desulfurization and dearomatization may not be exhibited. is there.
  • the hydrogen partial pressure is preferably from 3 to 8 MPa, more preferably from 3.5 to 7 MPa, and even more preferably from 4 to 6.5 MPa. If the hydrogen partial pressure is lower than 3 MPa, there is a concern that the effects of desulfurization and dearomatization may not be exhibited. If the hydrogen partial pressure is higher than 8 MPa, a large capital investment, such as reviewing the compressor and equipment strength, is required. It is possible that it is not desirable.
  • the reaction temperature is preferably from 280 to 380 ° C. If the reaction temperature is lower than 280 ° C., a sufficient desulfurization reaction rate or aromatic hydrogenation reaction rate may not be obtained, which is not preferable. On the other hand, if the temperature is higher than 380 ° C., it is not preferable because the hue of the produced oil may be deteriorated or the yield of the target fraction may be reduced due to decomposition.
  • the hydrogen-Z oil ratio (volume ratio) is preferably 50 to 500 NL / L.
  • the hydrogen / oil ratio indicates the ratio of the flow rate of the hydrogen gas to the flow rate of the feedstock oil. Since it can be removed outside the system, the reactivity tends to be improved. However, 500 NL When / L is exceeded, the reactivity is improved, but the effect is gradually reduced. In addition, there is a possibility that large capital investment such as a compressor is required. On the other hand, if it is less than 50 NLZL, the reactivity may decrease and the desulfurization / dearomatic reaction may not proceed sufficiently.
  • ⁇ 13 is preferably from 0.3 to 2.Oh'- 1 and more preferably from 0.35 to 0.35. ⁇ 1. 7 h " ⁇ more preferably from 0. 4 ⁇ 1. 2 h _1. L HSV is 2.
  • the catalyst and the contact time between the oil is for desulfurization short
  • the reaction may not proceed sufficiently, and the effect of desulfurization or dearomatization may not be exerted, and the reaction temperature is preferably 300 to 380 ° C. If the reaction temperature is lower than 300 ° C, a sufficient desulfurization reaction rate and Alternatively, it may not be possible to obtain an aromatic hydrogenation reaction rate, which is not preferable, and the hydrogen Z oil ratio is preferably 100 to 500 NL / L. And the progress of the desulfurization / dearomatization reaction may not be sufficient.
  • a presulfurization operation of the catalyst is performed.
  • the conditions for the presulfurization are not particularly limited, but the catalyst is generally in the form of an oxide of an active metal such as cobalt, nickel, and molybdenum :
  • the sulfur content of the petroleum-based hydrocarbon fraction and the sulfur content of the petroleum-based hydrocarbon fraction using a sulfurizing agent such as dimethyl disulfide are used to pass through the oil-based hydrocarbon fraction alone or to the fraction added with the sulfurizing agent.
  • a method is used in which the active metal is converted into a sulfide state by giving a temperature of at least ° C.
  • the type of reaction in the reaction tower in hydrodesulfurization is not particularly limited, but usually, a process such as a fixed bed or a moving bed is used. The fixed bed is preferred, and both the downflow and the upflow can be adopted for the feedstock distribution method.
  • the ultra-low sulfur / low aromatic gas oil produced when the gas oil fraction is subjected to the hydrodesulfurization treatment of the present invention may be used alone as a diesel gas oil.
  • Components such as a base material can be mixed and used as diesel light oil.
  • the kerosene fraction generated when the hydrodesulfurization treatment of the present invention is performed on the kerosene fraction can be used as diesel light oil.
  • the catalyst of the present invention has an extremely high desulfurization activity and can achieve an extremely high desulfurization depth of 10 mass ppm or less of sulfur content.
  • nitrogen compounds that are inhibitors of the desulfurization reaction also have high nitrogen resistance.
  • Water glass No. 3 was added to 1 kg of a 5% by mass aqueous sodium aluminate solution, and the mixture was placed in a container kept at 70 ° C. Preparation In a separate vessel the concentration 2. was added to 5 mass% of sulfuric acid Aruminiumu 'aqueous 11 ⁇ g of titanium sulfate (IV) solution (T i 0 24 wt% as 2 content) was kept at 70 ° C Then, it was added dropwise to the above-mentioned aqueous solution containing sodium aluminate for 15 minutes. The amounts of the water glass and the aqueous solution of titanium sulfate were adjusted so as to have predetermined silica and titania contents.
  • the cake-like slurry was transferred to a vessel equipped with a reflux condenser, 30 Om 1 of distilled water and 3 g of a 27% aqueous ammonia solution were added, and the mixture was heated and stirred at 70 ° C for 24 hours.
  • the slurry was put in a kneading apparatus, and heated to 80 ° C. or higher and kneaded while removing moisture to obtain a clay-like kneaded material.
  • the obtained kneaded material was extruded into a cylinder having a diameter of 1.5 mm by an extruder, dried at 110 ° C. for 1 hour, and calcined at 550 ° C. to obtain a molded carrier.
  • a molded carrier Take 300 g of the obtained molded carrier, add molybdenum trioxide, cobalt (II) nitrate hexahydrate, phosphoric acid (concentration: 85%) to 15 Om1 of distilled water, and add malic acid until dissolved. Impregnation was performed while spraying the prepared impregnation solution.
  • the amounts of molybdenum trioxide and cobalt nitrate (II) hexahydrate phosphoric acid used were adjusted so as to achieve the prescribed loading.
  • the impregnated sample was dried at 110 ° C for 1 hour and calcined at 550 ° C to obtain catalyst A.
  • Table 1 shows the physical properties of the prepared catalyst. (Example 2)
  • Example 1 the amounts of cobalt nitrate (II) hexahydrate and molybdenum trioxide were adjusted to predetermined values, and a catalyst B was obtained in the same manner as in Example 1. Table 1 shows the physical properties of the prepared catalyst.
  • Water glass No. 3 was added to 1 kg of an aqueous solution of sodium aluminate having a concentration of 5% by mass, and the mixture was placed in a container kept at 70 ° C. 1 kg of an aqueous solution of aluminum sulfate having a concentration of 2.5% by mass was placed in another container kept at 70 ° C., and added dropwise to the aqueous solution containing sodium aluminate for 15 minutes. The amount of water glass was adjusted to a predetermined silica content. The time when the pH of the mixed solution reached 6.9 to 7.5 was defined as the end point, and the obtained slurry-like product was filtered through a filter to obtain a cake-like slurry.
  • the cake slurry was transferred to a vessel equipped with a reflux condenser, 30 Om1 of distilled water and 3 g of a 27% aqueous ammonia solution were added, and the mixture was heated and stirred at 70 ° C for 24 hours.
  • the slurry was placed in a kneading apparatus, heated to 80 ° C. or higher, and kneaded while removing moisture to obtain a clay-like kneaded material.
  • the obtained kneaded product was extruded into a cylinder having a diameter of 1.5 mm using an extruder, dried at 110 ° C for 1 hour, and calcined at 550 ° C to obtain a molded carrier.
  • Catalyst D was obtained in the same manner as in Example 3, except that nickel nitrate hexahydrate was used instead of cobalt (II) nitrate hexahydrate used in Example 3. The amount of nitric acid nickel hexahydrate used was adjusted so as to be a predetermined amount supported. (Comparative Example 1)
  • Example 3 Take 300 g of the shaped carrier obtained in Example 3. Add 150 g of distilled water to 50 ml of distilled water, add molybdenum trioxide, cobalt nitrate (II) hexahydrate, and phosphoric acid (concentration: 85%), and dissolve malic acid until dissolved. was impregnated while spraying the impregnating solution prepared. The amounts of molybdenum trioxide and cobalt (II) nitrate hexahydrate phosphoric acid used were adjusted so as to have a prescribed amount. The impregnated sample was dried at 110 ° C for 1 hour and calcined at 550 ° C to obtain catalyst X. Table 1 shows the physical properties of the prepared catalyst.
  • the cake slurry was transferred to a vessel equipped with a reflux condenser, 150 ml of distilled water and 10 g of a 27% aqueous ammonia solution were added, and the mixture was heated and stirred at 80 ° C for 24 hours.
  • the slurry was placed in a kneading apparatus and heated to 80 ° C. or higher and kneaded while removing water to obtain a clay-like kneaded material.
  • the obtained kneaded product was extruded into a cylinder having a diameter of 1.5 mm by an extruder, dried at 110 ° C for 1 hour, and calcined at 550 ° C to obtain a molded carrier.
  • Example 5 50 g of the shaped carrier obtained in Example 5 was placed in an eggplant-shaped flask, and while degassing with a Rotary evaporator, 17.0 g of molybdenum trioxide and 13.2 g of nickel (II) nitrate hexahydrate were obtained. , Phosphoric acid (concentration 85%) 3.9 g and malic acid 4.0 g The impregnation solution was poured into the flask. The impregnated sample was dried at 120 ° C for 1 hour, and calcined at 550 ° C to obtain catalyst F. Table 2 shows the physical properties of the prepared catalyst F.
  • the cake-like slurry was transferred to a vessel equipped with a reflux condenser, and 150 ml of distilled water and 10 g of a 27% aqueous ammonia solution were added thereto, followed by heating and stirring at 80 ° C for 24 hours.
  • the slurry was placed in a kneading apparatus and heated to 80 ° C. or higher and kneaded while removing moisture to obtain a clay-like kneaded material.
  • the obtained kneaded material was extruded into a cylinder having a diameter of 1.5 mm by an extruder, dried at 110 ° C for 1 hour, and calcined at 550 ° C to obtain a molded carrier.
  • Example 6 50 g of the shaped carrier obtained in Example 6 was placed in an eggplant-shaped flask, and while degassing with a rotary evaporator, 16.6 lg of molybdenum trioxide, 19.0 g of cobalt nitrate ( ⁇ ) hexahydrate, 19.0 g of phosphoric acid An impregnating solution containing 1.9 g (concentration 85%) and 5.0 g of malic acid was injected into the flask. The impregnated sample was dried at 120 ° C for 1 hour, and then calcined at 550 ° C to obtain catalyst Y. Table 2 'shows the physical properties of the prepared catalyst Y. (Comparative Example 3)
  • the cake-like slurry was transferred to a vessel equipped with a reflux condenser, 150 ml of distilled water and 10 g of a 27% aqueous ammonia solution were added, and the mixture was heated and stirred at 80 ° C for 24 hours.
  • the slurry was placed in a kneading apparatus, heated to 80 ° C. or higher, and kneaded while removing water to obtain a clay-like kneaded material.
  • the obtained kneaded material was extruded into a cylinder having a diameter of 1.5 mm by an extruder, dried at 110 ° C for 1 hour, and calcined at 550 ° C to obtain a molded carrier. .
  • a reaction tube with an inner diameter of 15 mm is filled with 2 Om 1 of catalyst A, and a straight-run gas oil (sulfur content of 3% by mass) is added with dimethyl disulfide so that the sulfur concentration becomes 3% by mass.
  • Preliminary sulfurization of the catalyst was performed for 4 hours under the conditions of an average catalyst layer temperature of 300 ° C, a hydrogen partial pressure of 5 MPa, an LHS V of 1 h to a hydrogen Z oil ratio of 20 ONL / L.
  • feed oil A (10% distillation point 210 ° C, 90% distillation point 342 ° ⁇ , sulfur content 1.00 mass%, nitrogen content 90 mass ppm), a Middle Eastern straight gas oil
  • Hydrodesulfurization was performed by passing oil under the conditions of a reaction temperature of 340 ° C, a pressure of 5.0 MPa, an LHS V of 1 to a hydrogen Z oil ratio of 200 NLZL. After that, the oil was passed through feedstock B (10% distillation point 232 ° C, 90% distillation point 349 ° C, sulfur content: 1.20 mass%, nitrogen content: 210 mass ppm) to perform hydrodesulfurization. A comparison was made between the case where the feed oil A was treated and the sulfur content of the generated oil.
  • Example 9 The same operation as in Example 9 was performed for each of the catalysts Y and Z. Table 4 shows these results.

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  • Organic Chemistry (AREA)
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Abstract

L'invention concerne un catalyseur d'hydrogénation et de désulfuration pouvant atteindre une profondeur de désulfuration remarquablement élevée de 10 ppm en masse ou inférieure à la teneur en soufre, présentant une activité de déazotation élevée et ayant une capacité de résistance à l'azote élevée par rapport aux composés azotés inhibant la réaction de désulfuration. L'invention concerne plus précisément un catalyseur d'hydrogénation et de désulfuration pour hydrocarbures de pétrole se caractérisant par le fait qu'un support poreux inorganique composé principalement d'alumine contient, comme métaux actifs, au moins un métal sélectionné dans le Groupe 8 et au moins un métal sélectionné dans le Groupe 6A du tableau périodique des éléments, selon un rapport molaire [oxyde de métal du Groupe 8] / [oxyde de métal du Groupe 6A] compris entre 0,105 et 0,265, la teneur en métaux du Groupe 6A en termes d'oxyde étant comprise entre 20 et 30 % en masse sur la base du poids du catalyseur.
PCT/JP2005/000435 2004-01-09 2005-01-07 Catalyseur d'hydrogenation et de desulfuration pour hydrocarbure de petrole et procede d'hydrogenation et de desulfuration utilisant ce catalyseur WO2005065823A1 (fr)

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US11/456,160 US20060249429A1 (en) 2004-01-09 2006-07-07 Hydrodesulfurization Catalyst for Petroleum Hydrocarbons and Process for Hydrodesulfurization Using the Same
KR1020067015820A KR101218947B1 (ko) 2004-01-09 2006-08-04 석유계 탄화수소의 수소화 탈황 촉매 및 수소화 탈황 방법

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JP2004-004768 2004-01-09
JP2004-216337 2004-07-23
JP2004216337A JP2006035052A (ja) 2004-07-23 2004-07-23 石油系炭化水素の水素化脱硫触媒および水素化脱硫方法

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RU2474474C1 (ru) * 2011-11-28 2013-02-10 Российская Федерация, От Имени Которой Выступает Министерство Промышленности И Торговли Российской Федерации Катализатор, способ его приготовления и способ получения малосернистого дизельного топлива

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RU2474474C1 (ru) * 2011-11-28 2013-02-10 Российская Федерация, От Имени Которой Выступает Министерство Промышленности И Торговли Российской Федерации Катализатор, способ его приготовления и способ получения малосернистого дизельного топлива

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